Medicine incubator base wastewater long-time-effect standard reaching treatment system

Abstract

The invention belongs to the field of wastewater treatment, and particularly relates to a medicine incubator base wastewater long-time-effect standard reaching treatment system. Comprising three units, namely a coupling pretreatment unit, a multi-effect modification unit and a powerful biochemical treatment unit. The treatment units are reasonably combined, the treatment efficiency is high, the process stability is good, the system cooperative treatment effect on various kinds of wastewater of the medicine incubator is embodied, the pretreatment coupling unit effectively combines the gas stripping unit, the desalting unit and the catalytic oxidation treatment unit, the existing treatment technological process is shortened, the treatment difficulty is reduced, and the treatment cost is reduced. The wastewater treatment cost is remarkably reduced, and the wastewater recycling rate is increased.

Description

Technical Field

[0001] The invention belongs to the field of wastewater treatment, and in particular relates to a long-term and standard-reaching wastewater treatment system for a pharmaceutical incubator base. Background Art

[0002] At present, with the resurgence of the pharmaceutical industry, the national pharmaceutical incubator base has become a gathering area for the research and development and pilot-scale production of pharmaceutical companies, among which CRO (contract research organization) and CDMO (contract research and development and production organization) companies are the main ones. The research and development and production of each company usually adopt intermittent and order-based production, and the types of products vary greatly, resulting in the instability of the water quality, water volume and types of pollutants in the wastewater. It is characterized by complex composition, many types of biological toxic pollutants, high COD concentration, high inorganic salt content, large fluctuations in water volume and quality, high concentrations of emulsions and oils, etc. It is one of the high-concentration organic wastewaters that are seriously polluted and difficult to treat. Many scholars at home and abroad have conducted a lot of research on the treatment of pharmaceutical wastewater, and various physical, chemical and biological methods have been widely used, including high-efficiency evaporators, electrocatalytic chemistry, special physical adsorption, special membrane separation, biogenetic technology, etc. For example, patent CN10301526 B has a relatively clear targeted treatment process for erythromycin thiocyanate wastewater. Patent CN105776746A introduces a comprehensive sewage treatment system for a petrochemical park. "Research on the application of ozone catalytic oxidation technology in comprehensive wastewater treatment in industrial parks" (Yu Bo et al. "Water Supply and Drainage", 2023, 49) studied the deep treatment effect of pharmaceutical and chemical wastewater.

[0003] The types of enterprises in the pharmaceutical incubator are mixed, mainly including pharmaceutical intermediates, fine chemicals, new materials, etc. The high-salt and high-concentration wastewater produced has not been reasonably collected and treated by classification, and it is common to mix it with domestic sewage. It is difficult to achieve effective environmental management in the incubator, and it is urgent to seek a reasonable wastewater treatment process route. The existing processes for treating such wastewater usually have certain technical defects: first, the current main application research is mainly aimed at medium and low concentration pharmaceutical wastewater of a certain type of product, and the treatment method has certain limitations; secondly, the treatment method of organic solvents in wastewater does not consider the mutual solubility between solvents and does not make effective classification and disposal; finally, the existing wastewater treatment process still has certain deficiencies in the connection between the physical and chemical section and the biochemical section, resulting in poor treatment effects and other problems. The existing technology can achieve standard discharge within a certain period of time, but it has not achieved efficient, resource-based, and long-term standard discharge.

[0004] The treatment of wastewater from pharmaceutical incubators still needs to find new treatment models to achieve the optimal combination of different technologies, realize the systematic treatment of chemical synthesis pharmaceuticals, biological fermentation pharmaceuticals, traditional Chinese medicines and domestic sewage among companies in the park, better realize the resource utilization of different types of pharmaceutical wastewater, and make the wastewater treatment in pharmaceutical incubators achieve long-term and standard discharge. Summary of the invention

[0005] The technical problem to be solved by the present invention is to overcome the shortcomings of the current wastewater treatment process of the pharmaceutical incubator base, such as the poor technical connection and the low resource recovery rate.

[0006] The purpose of the present invention is to provide a comprehensive and long-term treatment and discharge system for pharmaceutical incubator wastewater from point source treatment to system treatment. The treatment system is suitable for pharmaceutical incubator wastewater treatment, especially for comprehensive wastewater treatment in newly built parks with unified planning and layout.

[0007] The object of the present invention can be achieved by the following technical solutions: A long-term treatment system for wastewater from a pharmaceutical incubator base, characterized in that it includes three units, namely a coupled pretreatment unit, a multi-effect modification unit and a strong biochemical treatment unit: The coupling preprocessing unit comprises the following steps: 1) The wastewater from upstream enterprises enters the flotation equipment, and then 2‰ -4‰ flocculants are added to the wastewater. The oil and suspended flocs adhere to the microbubbles, forming scum in the flotation separation area and being discharged; 2) The wastewater treated in step 1) is divided into high boiling point type A with boiling point > 100°C and low boiling point type B with boiling point < 100°C according to the boiling points of the organic solvents contained in the wastewater. The two types of wastewater are treated separately: a) High boiling point Class A wastewater with boiling point > 100℃ enters the membrane system through the pipeline collection system to remove hardness ions. The wastewater concentrated by the membrane system enters the MVR evaporation system, and the gas stripping agent is introduced into the treated wastewater to make the two fully contact. The dissolved gas and volatile organic matter in the water are desorbed from the liquid phase and transferred to the gas phase through the gas-liquid interface, thereby achieving the purpose of removing pollutants, and then sent to the multi-effect modification unit. b) Low-boiling-point Class B wastewater with a boiling point of less than 100°C is pumped to the top of a packed stripping tower. The packed tower is filled with annular or spherical packings. The wastewater is evenly distributed on the top layer of the packing layer and flows from top to bottom. Compressed air is blown into the bottom of the tower by a blower and fully contacts with the dispersed droplets in the packing layer. The volatile organic matter in the wastewater is transferred to the gas phase. The air containing volatile organic matter is discharged from the top of the tower into the absorption tower to recover low-boiling-point organic matter. The treated water is collected at the bottom of the tower and sent to the multi-effect modification unit. The multi-effect modification unit comprises the following steps: The wastewater pretreated by the coupling pretreatment unit enters the temporary intermediate water tank and is pumped to the electrocatalytic oxidation reaction tank through a pipeline. The electrocatalytic oxidation reaction tank is provided with an electrocatalytic oxidation combination device. The electrocatalytic oxidation combination device is a titanium electrode. The electrode includes an anode and a cathode, wherein the cathode is a pure titanium electrode plate, and the anode is a titanium substrate with a rare metal attached as a catalyst. The powerful biochemical treatment unit comprises the following steps: After the desalination and solvent recovery of the coupled pretreatment unit and the multi-effect modification unit, the high-salinity and high-concentration chemical pharmaceutical wastewater is collected and enters the comprehensive regulating tank. The effluent from the regulating tank enters the aerobic multiplication detoxification tank. Specific and efficient bacteria are added to the tank body of the aerobic multiplication detoxification tank, and strong water circulation is used to reduce the toxicity of organic matter to biological bacteria. The detoxified organic wastewater enters the hydrolysis acidification tank, and after 8-12 hours of treatment, it enters the two-stage AO treatment unit for treatment, thereby obtaining wastewater that meets the drainage requirements of the pharmaceutical and chemical industry.

[0008] Furthermore, the flocculant in the coupling pretreatment unit includes polyferric sulfate, polyaluminium sulfate or a combination thereof.

[0009] Furthermore, the surface load of the air flotation separation zone in the coupling pretreatment unit is 4-6m 3 / m 2. .h, residence time 20-30 minutes. After being treated by this treatment unit, most of the suspended solids and a small amount of oily organic matter in the wastewater are removed, and the COD removal rate reaches 20-30%.

[0010] Furthermore, the MVR system uses a set of MVR centrifugal compressor evaporators and a set of MVR mixed flow forced circulation evaporators in combination, the boiling point is increased by less than 5°C, the MVR centrifugal compressor evaporator is used to pressurize the secondary steam for evaporation, the secondary steam temperature is 88°C, and the secondary steam temperature in the MVR mixed flow forced circulation evaporator will be increased to 110-150°C, and the residual liquid mixed with organic solvent gas and brine is obtained, the organic solvent gas is circulated to the steam-water separator unit, and the residual liquid mixed with brine is subjected to brine separation treatment. After MVR evaporation treatment, the desalination efficiency reaches 99%.

[0011] Furthermore, in the coupled pretreatment unit, the salt obtained by evaporation is refined and used in the production of the cold salt bath cooling process, and the impurity salt that cannot be refined and recovered is harmlessly treated in an incinerator above 1100°C and landfilled.

[0012] The salt obtained by evaporation is mainly NaCl and Na2SO4.

[0013] Furthermore, some volatile components generated by the steam-water separator treatment unit can be directly used in the workshop production process, and the generated condensed steam temperature is used as the steam source of MVR. The terminal steam generated by the MVR steam-water separation is used as waste heat through the aerobic multiplication detoxification tank and the coil heat exchanger set in the AO tank body, thereby realizing the resource utilization of volatile components and water.

[0014] Furthermore, in the coupled pretreatment unit, the membrane system includes a microfiltration, ultrafiltration and reverse osmosis system or a combination thereof.

[0015] Furthermore, in the coupling pretreatment unit, the membrane system is made of PVDF nanofiltration membrane system, and the operating pressure of the nanofiltration membrane system is 0.1-0.25MP. The nanofiltration membrane has good separation performance for organic small molecules with molecular weight of hundreds in water, and has good performance for ions CO3 that cause scaling. 2－ , Ca 2+ Mg 2+ 、SO4 2－ , Fe 2+ The removal efficiencies of isovalent 2+ examples were 82%-85%, 95%-98%, 96%-98%, 95%-97% and 99%-99.8%, respectively.

[0016] Furthermore, in the coupling pretreatment unit, the boiling point increase range is controlled to be within 3°C.

[0017] Furthermore, in the coupled pretreatment unit, the stripping agent includes air, nitrogen, carbon dioxide or saturated steam, and the organic matter in different boiling ranges is desolvated by controlling the evaporation temperature in stages, thereby reducing the processing load of the subsequent process. The stripping agent is introduced into the treated wastewater to make the two fully contact, and the dissolved gas and volatile organic matter in the water are desorbed from the liquid phase and transferred to the gas phase through the gas-liquid interface, thereby achieving the purpose of removing pollutants, and then sent to the multi-effect modification unit.

[0018] In the coupled pretreatment unit, the recovered low-boiling point organic matter (including methanol / ethanol) is refined in the subsequent workshop and then reused in part of the workshop production process units, and the other part is used as an additional carbon source for the denitrification denitrification process.

[0019] Furthermore, in the coupled pretreatment unit, the terminal steam generated by the MVR steam-water separation is used as waste heat by means of a coil-type heat exchanger arranged in the aerobic multiplication detoxification tank and the AO tank, thereby reducing the use of fresh steam in the biochemical section and lowering costs.

[0020] In the multi-effect modification unit, the principle of the electrocatalytic oxidation method is to utilize the high oxidation potential of the anode material or the free radicals with strong oxidation ability (such as hydroxyl radicals, etc.) generated in the anode reaction to achieve effective pretreatment of high-salinity and high-concentration organic wastewater.

[0021] Furthermore, the catalyst in the multi-effect modification unit includes a combination of titanium and ruthenium-iridium, a combination of titanium and iridium-tantalum, or a combination of titanium and platinum.

[0022] The current density of the catalytic oxidation treatment is 1-60 mA / cm 2 , preferably 2-20mA / cm 2 .

[0023] The voltage of the catalytic oxidation treatment is 3-20V, preferably 5-8V.

[0024] The catalytic oxidation treatment residence time is 30-120 min, preferably 30-60 min.

[0025] The core reactor is made of PP material.

[0026] The combination of the anode electrode plates is titanium-ruthenium-iridium intermittently connected in series with titanium-iridium-tantalum, forming a series catalytic electric field voltage fluctuation change.

[0027] Furthermore, in the multi-effect modification unit, the electrocatalytic oxidation combination device is a 4-cathode + 3-anode device, including four cathodes made of pure titanium, two anodes made of titanium-ruthenium-iridium, and one anode made of titanium-iridium-tantalum. The cathodes and anodes are arranged at intervals, and the titanium-iridium-tantalum anode is located in the middle.

[0028] After passing through the electrocatalytic system, the toxicity of the wastewater is greatly reduced, the biodegradability of the wastewater is improved, and the main product is short-chain organic matter.

[0029] Furthermore, the water circulation ratio in the powerful biochemical treatment unit reaches 50-100 times, and the steam-water ratio reaches 150:1.

[0030] Furthermore, the dissolved oxygen of the wastewater in the O section (aerobic short) of the two-stage AO treatment unit is maintained at 3-5 mg / L, wherein AOB bacteria (ammonia oxidizing bacteria) are added in the A (anoxic section) and NOB bacteria (nitrite bacteria) are added in the O section (aerobic short). The COD removal rate of the wastewater treated by the hydrolysis unit can reach 10%-20%.

[0031] The addition of AOB and NOB strains reduces the residence time of ammonia nitrogen removal.

[0032] The ammonia nitrogen removal rate of the wastewater treated by the two-stage AO process is 97-98%, the total nitrogen removal rate is 75-80%, and the COD removal rate is 85-95%, which meets the drainage requirements of the pharmaceutical and chemical industry.

[0033] The above-mentioned pharmaceutical incubator wastewater long-term standard comprehensive discharge system of the present invention is simple, compact and efficient to operate through technical integration, has a wide range of applications, and can maximize the resource utilization and ultra-low emission of high-salt and high-concentration organic wastewater from pharmaceutical incubators. Compared with the existing pharmaceutical incubator wastewater treatment method, the treatment method of the present invention has the following outstanding advantages: (1) The treatment units of the present invention are reasonably combined, with high treatment efficiency and good process stability, reflecting the system synergistic treatment effect of various types of wastewater from pharmaceutical incubators. The pretreatment coupling unit of the present invention effectively combines the gas stripping unit, the desalination unit and the catalytic oxidation treatment unit, shortens the process flow of the existing treatment, reduces the treatment difficulty, significantly reduces the cost of wastewater treatment, and improves the reuse rate of wastewater. (2) The residual secondary steam of the pretreatment coupling unit of the present invention can be utilized as waste heat by arranging a coil heat exchanger inside the biochemical system, thereby reducing the input of new steam in the biochemical section and thus reducing the treatment cost.

[0034] (3) The present invention preferably uses nanofiltration membrane in the pretreatment unit, which not only removes scaling ions, but also reduces the introduction of metal ions in traditional exogenous antiscalants, thereby alleviating the processing load of the MVR process.

[0035] (4) The present invention strengthens the treatment of pollution at the source and strengthens the reuse of materials. According to the sources of wastewater from different enterprises, the valuable components are recovered as single salts through separation methods such as gas, etc. For example, the recovered NaCl and Na2SO4 are used for cold salt bath in the production unit, and the recovered methanol and ethanol are used as external carbon sources for denitrification and denitrification in the back-end sewage deep treatment. Useful resources are effectively utilized. At the same time, the removal of inorganic salts and the significant reduction of the organic matter content in the wastewater reduce the difficulty of downstream sewage treatment processes.

[0036] (5) The present invention proposes for the first time a multi-stage series combination method of attaching different metal electrode plates. This combination method gives full play to the specificity of different electrodes in treating different organic matter, so that different groups of aromatic compounds and various heterocyclic organic matter are dissociated and mineralized in an orderly and efficient manner, reducing biological toxicity. The new combination method of electrode plates improves the broad-spectrum applicability of the process and increases the types of wastewater that can be treated.

[0037] (6) The present invention is the first to establish an aerobic biological multiplication detoxification pool. Through a large steam-water ratio and reflux ratio, the toxicity of the pretreated wastewater is further reduced by the volatilization of a portion of the wastewater during the flow process, and the biological toxic substances are further reduced. Compared with the traditional method of directly entering anaerobic treatment into the pretreated wastewater, the patent of the present invention significantly shortens the residence time of the subsequent AO process, greatly reduces the civil engineering pool capacity, and saves engineering investment.

[0038] (7) The present invention improves the impact resistance and treatment efficiency of the biochemical system by adding different specific and efficient strains to the biological treatment unit. The specific combination of strains has the characteristics of strong specificity and high treatment efficiency. As a pre-process pretreatment process, the aerobic multiplication tank is superior to the traditional "anaerobic + aerobic" mode, making the treatment mode become the "aerobic-anaerobic-aerobic" mode, and the impact resistance is better than the existing method. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Attached Figure 1 This is a flow chart of the long-term treatment system for wastewater from a high-boiling-point pharmaceutical incubator base containing organic solvents with a boiling point greater than 100°C; Attached Figure 2 Figure 2 is a diagram of the electrocatalytic electrode combination. DETAILED DESCRIPTION

[0040] Embodiment 1 like Figure 1 As shown, Figure 1 This is a flow chart of the long-term treatment system for wastewater from a high-boiling-point pharmaceutical incubator base containing organic solvents with a boiling point of more than 100°C, which includes three units, namely "coupled pretreatment unit - multi-effect modification unit - strong biochemical treatment unit", referred to as the PC-BIO system. Among them, P stands for the pre-coupling treatment unit; C stands for the multi-effect modification unit; and BIO stands for the strong biochemical treatment unit.

[0041] The coupling preprocessing unit comprises the following steps: 1) The wastewater from the upstream enterprises enters the 1 flotation equipment, and then 2‰ -4‰ flocculants are added to the wastewater. The oil and suspended flocs adhere to the microbubbles, forming scum in the flotation separation area and are discharged.

[0042] The flocculant is polyferric sulfate, polyaluminium sulfate or a combination thereof.

[0043] In the above steps, the surface load of the air flotation separation zone is 4-6m 3 / m 2. .h, residence time 20-30 minutes. After being treated by this treatment unit, most of the suspended solids and a small amount of oily organic matter in the wastewater are removed, and the COD removal rate reaches 20-30%.

[0044] 2) High-boiling-point Class A wastewater with a boiling point greater than 100°C enters the 2 membrane system through a pipeline collection system to remove hardness ions; the wastewater concentrated by the membrane system enters the 3MVR evaporation system.

[0045] Furthermore, in order to reduce the operating cost of the MVR evaporation system, the MVR system uses a set of MVR centrifugal compressor evaporators and a set of MVR mixed flow forced circulation evaporators in combination, and the boiling point is increased by less than 5°C. The MVR centrifugal compressor evaporator is used to pressurize the secondary steam and evaporate it. The secondary steam temperature is 88°C. In the MVR mixed flow forced circulation evaporator, the secondary steam temperature will be increased to 110-150°C to obtain a residual liquid mixed with organic solvent gas and brine; the organic solvent-containing gas is circulated to the steam-water separator unit, and the residual liquid mixed with brine is subjected to brine separation treatment. After MVR evaporation treatment, the desalination efficiency reaches 99%.

[0046] The salt obtained by evaporation is mainly NaCl and Na2SO4. After refining, it is used in the production of cold salt bath cooling process. The impurity salt that cannot be refined and recovered is harmlessly treated in an incinerator above 1100℃ and landfilled.

[0047] Part of the volatile components produced by the steam-water separator processing unit can be directly returned to the workshop production workshop. The generated condensed steam temperature is 80°C-90°C and can be used as the steam source of MVR. The terminal steam produced by the MVR steam-water separation is used as waste heat through the coil-type heat exchanger arranged in the aerobic multiplication detoxification tank and the AO tank body, thereby realizing the resource utilization of volatile components and water.

[0048] The stripping agent is introduced into the wastewater treated in step 2) to make the two fully contact, and the dissolved gas and volatile organic matter in the water are desorbed from the liquid phase and transferred to the gas phase through the gas-liquid interface, thereby achieving the purpose of removing pollutants, and then sent to the multi-effect modification unit.

[0049] The membrane system can be a microfiltration, ultrafiltration and reverse osmosis system or a combination thereof, and the preferred material is a PVDF (polyvinylidene fluoride) nanofiltration membrane system. The operating pressure of the nanofiltration membrane system is 0.1-0.25MP. The nanofiltration membrane has good separation performance for organic small molecules with molecular weights of hundreds in water, and has good performance for ions CO3 that cause scaling. 2－ , Ca 2+ Mg 2+ 、SO4 2－ , Fe 2+ The removal efficiencies of isovalent 2+ examples were 82%-85%, 95%-98%, 96%-98%, 95%-97% and 99%-99.8%, respectively.

[0050] The boiling point increase range controls the temperature to be within 3°C.

[0051] The stripping agent includes air, nitrogen, carbon dioxide or saturated steam, preferably saturated steam, and organic matter with different boiling ranges is desolvated by controlling the evaporation temperature in stages, thereby reducing the processing load of subsequent processes.

[0052] The wastewater treated by the coupled pretreatment unit is sent to the multi-effect modification unit, which includes the following steps: The pretreated wastewater enters the temporary storage 4 intermediate water tank and is pumped to the 5 electrocatalytic oxidation reaction tank through a pipeline.

[0053] The principle of electrocatalytic oxidation is to utilize the high oxidation potential of the anode material or the free radicals with strong oxidizing ability (such as hydroxyl radicals, etc.) produced in the anode reaction to achieve effective pretreatment of high-salinity and high-concentration organic wastewater.

[0054] The electrocatalytic oxidation combined device of "4 cathodes + 3 anodes" is selected for catalytic oxidation treatment. Figure 2 As shown, No. 1 is a cathode made of pure titanium; No. 2 and No. 4 are anodes made of titanium-ruthenium-iridium, and No. 3 is an anode made of titanium-iridium-tantalum. After passing through the electrocatalytic system, the toxicity of the wastewater is greatly reduced, the biodegradability of the wastewater is improved, and the main degradation products are short-chain organic substances.

[0055] The current density of the catalytic oxidation treatment is 1-60 mA / cm 2 , preferably 2-20mA / cm 2 .

[0056] The voltage of the catalytic oxidation treatment is 3-20V, preferably 5-8V.

[0057] The catalytic oxidation treatment residence time is 30-120 min, preferably 30-60 min.

[0058] The core reactor is made of PP material.

[0059] The enhanced biochemical treatment unit described above comprises the following steps: After the desalination and solvent recovery of the coupled pretreatment unit and the multi-effect modification unit, the toxicity of high-salinity and high-concentration chemical pharmaceutical wastewater is significantly reduced and the biodegradability is significantly improved.

[0060] After collection, it enters the 6th comprehensive regulating pool, and the effluent of the regulating pool enters the 7th aerobic multiplication detoxification pool. Specific and efficient bacteria are added to the pool body, and strong water circulation is used to reduce the toxicity of organic matter to biological bacteria. The circulation ratio reaches 50-100 times, and the steam-water ratio reaches 150:1. The detoxified organic wastewater enters the 8th hydrolysis acidification pool, and after 8-12 hours of treatment, it enters the 9th two-stage AO treatment. The COD removal rate of the wastewater treated by the hydrolysis unit can reach 10%-20%.

[0061] The dissolved oxygen of the O section (aerobic short) wastewater in the two-stage AO treatment unit is maintained at 3-5 mg / L, wherein AOB bacteria (ammonia oxidizing bacteria) are added to the A (anoxic section) and NOB bacteria (nitrite bacteria) are added to the O section (aerobic short).

[0062] The addition of AOB and NOB strains reduces the residence time of ammonia nitrogen removal.

[0063] The wastewater treated by the two-stage AO process has an ammonia nitrogen removal rate of 97-98%, a total nitrogen removal rate of 75-80%, and a COD removal rate of 85-95%. It is discharged through 10 clear water tanks and meets the drainage requirements of the pharmaceutical and chemical industry.

[0064] The added specific high-efficiency bacteria include DMF (N, N-dimethylformamide) specific degradation bacteria or tetrahydrofuran specific degradation bacteria.

[0065] Embodiment 2 This embodiment provides a process of a comprehensive discharge system for wastewater from a pharmaceutical incubator that meets the standards for a long term, in combination with the first embodiment. Figure 1 As shown, the specific steps include: (1) The total amount of workshop production wastewater is 100m 3 / d, high-salt wastewater with a COD content of 80,000 mg / L and a salt content of 10% first enters a flotation device to remove suspended solids and oily matter. The flotation effluent is pumped into a membrane system 2 for hardness removal, and the nanofiltration membrane is used for concentration to remove calcium, magnesium and other ions. The concentrated liquid enters a 3MVR evaporation and desalination system. The evaporation treatment temperature is 110°C and the treatment time is 2 hours. After brine separation, the NaCl and Na2SO4 separated liquids have a salt content of 1000-2000 mg / L.

[0066] (2) The evaporated wastewater obtained in step (1) is temporarily stored in the intermediate water tank 4 and pumped into the multi-effect modification system 5 through a pipeline for electrocatalysis, with a current density of 10 mA / cm 2 , voltage is 5V, and residence time is 40min.

[0067] (3) The wastewater from step (2) is homogenized and mixed in the 6th comprehensive regulating tank, and then enters the 7th aerobic multiplication detoxification tank for treatment. The effluent enters the 8th hydrolysis acidification tank and stays there for 10 hours. Then it enters the 9th two-stage AO treatment unit.

[0068] (4) In the AO treatment unit, the dissolved oxygen of the wastewater is maintained at 3-5 mg / L, and the wastewater is retained for 36 hours. The ammonia nitrogen removal rate at this stage is 96%, the COD removal rate is 90%, and the COD and NH3-N of the aerobic effluent are 105 mg / L and 3 mg / L respectively. The effluent is discharged through 10 clear water tanks to meet the standards.

Claims

1. A long-term treatment system for wastewater from a pharmaceutical incubator base, characterized in that: It includes three units, namely, coupling pretreatment unit, multi-effect modification unit and strong biochemical treatment unit: The coupling preprocessing unit comprises the following steps: 1) The wastewater from upstream enterprises enters the flotation equipment, and then 2‰ -4‰ flocculants are added to the wastewater. The oil and suspended flocs adhere to the microbubbles, forming scum in the flotation separation area and being discharged; 2) The wastewater treated in step 1) is divided into high boiling point type A with boiling point > 100°C and low boiling point type B with boiling point < 100°C according to the boiling points of the organic solvents contained in the wastewater. The two types of wastewater are treated separately: a) High boiling point Class A wastewater with boiling point > 100℃ enters the membrane system through the pipeline collection system to remove hardness ions. The wastewater concentrated by the membrane system enters the MVR evaporation system, and the gas stripping agent is introduced into the treated wastewater to make the two fully contact. The dissolved gas and volatile organic matter in the water are desorbed from the liquid phase and transferred to the gas phase through the gas-liquid interface, thereby achieving the purpose of removing pollutants, and then sent to the multi-effect modification unit. b) Low-boiling-point Class B wastewater with a boiling point of less than 100°C is pumped to the top of a packed stripping tower. The packed tower is filled with annular or spherical packings. The wastewater is evenly distributed on the top layer of the packing layer and flows from top to bottom. Compressed air is blown into the bottom of the tower by a blower and fully contacts with the dispersed droplets in the packing layer. The volatile organic matter in the wastewater is transferred to the gas phase. The air containing volatile organic matter is discharged from the top of the tower into the absorption tower to recover low-boiling-point organic matter. The treated water is collected at the bottom of the tower and sent to the multi-effect modification unit. The multi-effect modification unit comprises the following steps: The wastewater pretreated by the coupling pretreatment unit enters the temporary intermediate water tank and is pumped to the electrocatalytic oxidation reaction tank through a pipeline. The electrocatalytic oxidation reaction tank is provided with an electrocatalytic oxidation combination device. The electrocatalytic oxidation combination device is a titanium electrode. The electrode includes an anode and a cathode, wherein the cathode is a pure titanium electrode plate, and the anode is a titanium substrate with a rare metal attached as a catalyst. The powerful biochemical treatment unit comprises the following steps: After the desalination and solvent recovery of the coupled pretreatment unit and the multi-effect modification unit, the high-salinity and high-concentration chemical pharmaceutical wastewater is collected and enters the comprehensive regulating tank. The effluent from the regulating tank enters the aerobic multiplication detoxification tank. Specific and efficient bacteria are added to the tank body of the aerobic multiplication detoxification tank, and strong water circulation is used to reduce the toxicity of organic matter to biological bacteria. The detoxified organic wastewater enters the hydrolysis acidification tank, and after 8-12 hours of treatment, it enters the two-stage AO treatment unit for treatment, thereby obtaining wastewater that meets the drainage requirements of the pharmaceutical and chemical industry.

2. A pharmaceutical incubator wastewater long-term treatment system as claimed in claim 1, characterized in that: In the coupling pretreatment unit, the MVR system uses a set of MVR centrifugal compressor evaporators and a set of MVR mixed flow forced circulation evaporators for use in combination, the boiling point is increased by less than 5°C, the secondary steam is pressurized by the MVR centrifugal compressor evaporator and evaporated, the secondary steam temperature is 88°C, and the secondary steam temperature in the MVR mixed flow forced circulation evaporator will be increased to 110-150°C to obtain a residual liquid mixed with a vapor containing an organic solvent and brine, the vapor containing the organic solvent is circulated to the steam-water separator unit, the residual liquid mixed with the brine is subjected to brine separation treatment, the evaporated salt is refined and used in the production of cold salt bath cooling process, and the miscellaneous salts that cannot be refined and recovered are harmlessly treated in an incinerator above 1100°C and landfilled.

3. A long-term treatment system for wastewater from a pharmaceutical incubator base as claimed in claim 1, characterized in that: In the coupled pretreatment unit, part of the volatile components generated by the steam-water separator treatment unit can be directly used in the workshop production process, and the generated condensed steam temperature is used as the steam source of the MVR, thereby realizing the resource utilization of volatile components and water.

4. A long-term treatment system for wastewater from a pharmaceutical incubator base as claimed in claim 1, characterized in that: In the coupled pretreatment unit, the stripping agent includes air, nitrogen, carbon dioxide or saturated steam, and the organic matter in different boiling ranges is desolvated by controlling the evaporation temperature in stages, thereby reducing the processing load of subsequent processes.

5. The pharmaceutical incubator wastewater long-term treatment system as claimed in claim 1, characterized in that: In the coupled pretreatment unit, the terminal steam generated by the MVR steam-water separation utilizes the waste heat through the coil-type heat exchanger arranged in the aerobic multiplication detoxification tank and the AO tank.

6. The pharmaceutical incubator wastewater long-term treatment system as claimed in claim 1, characterized in that: The catalyst in the multi-effect modification unit includes a combination of titanium and ruthenium-iridium, a combination of titanium and iridium-tantalum, or a combination of titanium and platinum.

7. The pharmaceutical incubator wastewater long-term treatment system as claimed in claim 1, characterized in that: In the multi-effect modification unit, the electrocatalytic oxidation combination device is a 4-cathode + 3-anode device, including four cathodes made of pure titanium, two anodes made of titanium-ruthenium-iridium, and one anode made of titanium-iridium-tantalum. The cathodes and anodes are arranged at intervals, and the titanium-iridium-tantalum anode is located in the middle.

8. The pharmaceutical incubator wastewater long-term treatment system as claimed in claim 1, characterized in that: The water circulation ratio in the enhanced biochemical treatment unit reaches 50-100 times, and the steam-water ratio reaches 150:

1.

9. The pharmaceutical incubator wastewater long-term treatment system as claimed in claim 1, characterized in that: The dissolved oxygen of the wastewater in the O section of the two-stage AO treatment unit in the enhanced biochemical treatment unit is maintained at 3-5 mg / L, wherein AOB bacteria are added to the A section and NOB bacteria are added to the O section. The specific and efficient bacteria in the enhanced biochemical treatment unit include N, N-dimethylformamide specific degradation bacteria or tetrahydrofuran specific degradation bacteria.

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